Hydroformylation process employing a cobalt-based catalyst in a non-aqueous liquid with improved catalyst recycling

ABSTRACT

A process for hydroformylating olefinically unsaturated compounds by means of a cobalt-based catalyst is carried out in a non-aqueous ionic liquid which is a liquid at a temperature below 90° C. and comprises at least one ammonium and/or phosphonium and/or sulfonium cation Q +  and at least one anion A − ; catalyst recycling is improved by using a ligand selected from the group consisting of Lewis bases and employing a depressurization step between the pressurized reaction step and the step for separating the phases by decanting. At the end of said depressurization step, the organic phase is separated in the decanting step and the non-aqueous ionic liquid containing the catalyst can be re-used.

This Application is A Divisional Of U.S. Ser. No. 10/411,389, Filed Apr.11, 2003 now U.S. Pat. No. 7,060,860.

FIELD OF THE INVENTION

The present invention relates to a process for hydroformylatingolefinically unsaturated compounds using a cobalt-based catalyst carriedout in a two-phase medium, with improved catalyst recycling. One of thephases comprises a non-aqueous ionic liquid comprising at least onequaternary ammonium and/or phosphonium and/or sulfonium cation Q⁺ and atleast one anion A⁻. The catalyst comprises at least one cobalt complex.

BACKGROUND OF THE INVENTION

Hydroformylating olefinic compounds is a reaction of great industrialimportance and the majority of processes employ homogeneous catalystsdissolved in an organic phase comprising the reagents, products andpossibly an excess of ligand, and so problems arise when separating andrecovering the catalyst, in particular when the catalyst is used inrelatively large quantities, as is the case with cobalt-based catalysts.

One solution to the problem has been mentioned by Bartik et al.:Organometallics (1993) 12, 164–170, J Organometal Chem (1994), 480,15–21, and by Beller et al.: J Molecular Catal A: Chemical (1999), 143,31–39. It consists of carrying out hydroformylation in the presence ofan aqueous solution containing a cobalt complex which is renderedwater-soluble by the presence of a phosphine-sulfonate ligand such asthe sodium salt of trisulfonated triphenylphosphine or a trisulfonatedtris(alkylphenyl)phosphine. International patent applicationWO-A-97/00132 describes cobalt clusters substituted bytrialkoxysilylmethyl groups which renders them water-soluble. In thatmanner, the organic phase containing the aldehydes is readily separatedfrom the aqueous phase containing the catalyst.

Despite the major industrial importance of said techniques forhydroformylating olefinic compounds, said two-phase systems suffer froma lack of solubility of the olefins in water, which results inrelatively low reaction rates and makes them inapplicable to long chainolefins.

Further, U.S. Pat. No. 3,565,823 describes a technique consisting ofdispersing a transition metal compound in a tin or germanium salt of aquaternary ammonium or phosphonium compound, with formula (R¹R²R³R⁴Z)YX₃in which R¹, R², R³ and R⁴ are hydrocarbyl groups containing up to 18carbon atoms, Z is nitrogen or phosphorus, Y is tin or germanium and Xis a halogen, either chlorine or bromine. U.S. Pat. No. 3,832,391describes a process for carbonylating olefins using the samecomposition. Those compositions suffer from the disadvantage of having arelatively high melting point, for example over 90° C., whichcomplicates manipulation of the solutions of catalyst and reactionproducts.

U.S. Pat. No. 5,874,638, commonly assigned, describes benefiting bothfrom employing two phases while avoiding the drawbacks due to usingwater, and from the use of compounds with high melting points bydissolving certain catalytic compounds of transition metals from groups8, 9 and 10, known to catalyse hydroformylation, in non-aqueous ionicliquids constituted by organic-inorganic salts that are liquid atambient temperatures. However, when the catalyst comprises a salt or acobalt complex, it is very difficult to prevent at least partialformation of dicobalt-octacarbonyl and/or cobalt-tetracarbonyl hydrideunder the hydroformylation reaction conditions. These two compounds arehighly soluble in the organic reaction phase constituted by at least theolefinic reagent and the aldehydes produced, and so recycling the cobaltusing the non-aqueous ionic liquid phase is only partial, causing lossof catalyst.

SUMMARY OF THE INVENTION

It has now been discovered that in the hydroformylation reactioncatalysed by cobalt complexes employed in a non-aqueous ionic liquidcomprising at least one ammonium and/or phosphonium and/or sulfoniumcation Q⁺ and at least one anion A⁻ which is liquid at a temperature ofless than 90° C., recycling the metal in the ionic liquid is greatlyimproved by using a ligand selected from the group consisting of Lewisbases and using an intermediate depressurization step between thepressurized reaction step and the step for separating the phases bydecanting. At the end of this depressurization step, the organic phaseis separated in the decanting step and the non-aqueous ionic liquidphase containing the catalyst can be re-used.

More precisely, the invention provides a process for liquid phasehydroformylation of olefinically unsaturated compounds, comprising apressurized reaction step carried out in the presence of at least onenon-aqueous ionic liquid comprising at least one salt with generalformula Q⁺ A⁻ in which Q⁺ represents a quaternary ammonium cation and/ora quaternary phosphonium cation and/or a quaternary sulfonium cation andA⁻ represents an anion, and a step for decanting the final products,said process being characterized in that the catalyst comprises at leastone complex of cobalt with at least one ligand selected from the groupconsisting of Lewis bases and in that an intermediate depressurizationstep is carried out between the reaction step and the decanting step.

Without wishing to be bound by any particular theory, under theconditions of the hydroformylation reaction pressurized with synthesisgas, most of the catalyst can be considered to be present in the form ofthe complexes Co₂(CO)₈, Co₂(CO)₆L₂, HCo(CO)₄ and HCo(CO)₃L in which L isthe Lewis base ligand, and in the step for depressurization prior tophase separation, the presence of the basic ligand L encourages theformation of ionic cobalt complexes such as (CoL₆)⁺⁺[Co(CO)₄ ⁻]₂ whichhave a high affinity for the phase containing the non-aqueous ionicliquid.

The non-aqueous ionic liquid is selected from the group consisting ofliquid salts with general formula Q⁺ A⁻ in which Q⁺ represents aquaternary ammonium and/or a quaternary phosphonium and/or quaternarysulfonium cation and A⁻ represents any anion that is capable of forminga liquid salt at low temperatures, i.e., below 90° C. and advantageouslyat most 85° C., and preferably below 50° C. Preferred anions A⁻ arenitrate, sulfate, phosphate, acetate, halogenoacetates,tetrafluoroborate, tetrachloroborate, tetraalkylborates,tetraarylborates, hexafluorophosphate, hexafluoroantimonate,fluorosulfonate ions, alkylsulfonates, perfluoroalkylsulfonates,bis(perfluoroalkylsulfonyl)amides and arenesulfonates, the latteroptionally being substituted with halogen or halogenoalkyl groups.

The quaternary ammonium and/or phosphonium cation(s) Q⁺ preferablyhas/have general formulae NR¹R²R³R⁴⁺ and PR¹R²R³R⁴⁺, or general formulaeR¹R²N═CR³R⁴⁺ in which R¹, R², R³ and R⁴, which may be identical ordifferent, represent hydrogen (with the exception of the cation NH₄ ⁺for NR¹R²R³R⁴⁺); preferably, a single substituent represents hydrogen,or hydrocarbyl groups containing 1 to 30 carbon atoms, for example alkylgroups that may or may not be saturated, cycloalkyl or aromatic groups,or aryl or aralkyl groups that may be substituted, containing 1 to 30carbon atoms. The ammonium and/or phosphonium cations can also bederived from nitrogen-containing and/or phosphorus-containingheterocycles containing 1, 2 or 3 nitrogen and/or phosphorus atoms inwhich the cycles are constituted by 4 to 10 atoms, preferably 5 or 6atoms.

The quaternary ammonium and phosphonium cations may also satisfy thefollowing formulae respectively:R¹R²⁺N═CR³—R⁵—R³C═N⁺R¹R² andR¹R²⁺P═CR³—R⁵—R³C═P⁺R¹R²in which R¹, R² and R³, which may be identical or different, are asdefined above, and R⁵ represents an alkylene or phenylene radical. Amonggroups R¹, R², R³ and R⁴, the radicals may be methyl, ethyl, propyl,isopropyl, butyl, secondary butyl, tertiary butyl, amyl, methylene,ethylidene, phenyl or benzyl; R⁵ may be a methylene, ethylene, propyleneor phenylene group.

The ammonium and/or phosphonium cation Q⁺ is preferably selected fromthe group formed by N-butylpyridinium, N-ethylpyridinium, pyridinium,3-ethyl-1-methylimidazolium, 3-butyl-1-methylimidazolium,3-hexyl-1-methylimidazolium, 3-butyl-1,2-dimethylimidazolium,diethylpyrazolium, N-butyl-N-methylpyrrolidinium,trimethylphenylammonium, tetrabutyl-phosphonium andtributyl-tetradecylphosphonium.

The sulfonium cations for use in the invention can have general formulaSR¹R²R³⁺, where R¹, R² and R³, which may be identical or different, eachrepresent a hydrocarbyl radical containing 1 to 12 carbon atoms, forexample an alkyl, saturated or unsaturated, cycloalkyl or aromatic,aryl, alkaryl or aralkyl group containing 1 to 12 carbon atoms.

Examples of salts that can be for use in the invention that can be citedare N-butylpyridinium hexafluorophosphate, N-ethyl pyridiniumtetrafluoroborate, pyridinium fluorosulfonate,3-butyl-1-methylimidazolium tetrafluoroborate,3-butyl-1-methylimidazolium hexafluoroantimonate,3-butyl-1-methylimidazolium hexafluorophosphate,3-butyl-1-methylimidazolium trifluoroacetate,3-butyl-1-methylimidazolium trifluoromethylsulfonate,3-butyl-1-methylimidazolium bis(trifluoromethylsulfonyl)amide,trimethylphenylammonium hexafluorophosphate and tetrabutylphosphoniumtetrafluoroborate. These salts may be used alone or as a mixture.

The catalyst cobalt compound precursors are selected from the groupconsisting of cobalt salts such as acetylacetonates, carboxylates and inparticular the formate or acetate, and carbonyl complexes such asdicobalt-octacarbonyl, cobalt-tetracarbonyl hydride and carbonylclusters. The choice of cobalt precursor compound is not critical butpreferably, halides are generally avoided.

The basic Lewis ligand is selected from the group consisting ofoxygen-containing ligands, sulfur-containing ligands,nitrogen-containing ligands and phosphorus-containing ligands, which mayor may not be substituted by ionic functional groups such as sulfonates,carboxylates, phosphates, ammonium and phosphonium compounds.

More particularly, the oxygen-containing ligands are selected from thegroup consisting of alcohols, phenols, ethers, ketones and acetals.Non-limiting examples that can be cited are methanol, ethanol, phenol,diethylether, dibutylether, diphenylether, tetrahydrofuran, 1,4-dioxane,1,3-dioxolane, glyme, diglyme, acetone, methylethylketone, acetophenone,methylal, 2,2-dimethoxypropane and 2,2-di(2-ethylhexyloxy)-propane.

More particularly, the sulfur-containing ligands are selected from thegroup consisting of thiols, thiophenols, thioethers and disulfides.Non-limiting examples that can be cited are methanethiol, ethanethiol,thiophenol, diethylsulfide, dimethyldisulfide and tetrahydrothiophene.

More particularly again, the nitrogen-containing ligands are selectedfrom the group consisting of monoamines, di-, tri- and poly-amines,imines, diimines, pyridines, bipyridines, imidazoles, pyrroles andpyrazoles. Non-limiting examples that can be cited are methylamine,trimethylamine, triethylamine, ethylenediamine, diethylenetriamine,diazabicyclooctane, N,N′-dimethylethane-1,2-diimine,N,N′-di-t-butylethane-1,2-diimine, N,N′-di-t-butylbutane-2,3-diimine,N,N′-diphenylethane-1,2-diimine,N,N′-bis-(2,6-dimethylphenyl)ethane-1,2-diimine,N,N′-bis-(2,6-diisopropylphenyl)ethane-1,2-diimine,N,N′-diphenylbutane-2,3-diimine,N,N′-bis-(2,6-dimethylphenyl)butane-2,3-diimine,N,N′-bis-(2,6-diisopropylphenyl)butane-2,3-diimine, pyridine,2-picoline, 4-picoline, t-butyl-2-pyridine, di-(t-butyl)-2,6-pyridine,2,2′-bipyridine, imidazole, N-methylimidazole, N-butylimidazole,pyrrole, N-methylpyrrole and 2,5-dimethylpyrrole.

More particularly, the phosphorus-containing ligands are selected fromthe group consisting of phosphines, polyphosphines, phosphine oxides andphosphites. Non-limiting examples that can be cited aretributylphosphine, triisopropylphosphine, tricyclohexylphosphine,triphenylphosphine, tris(o-tolyl) phosphine,bis(diphenylphosphino)ethane, trioctylphosphine oxide,triphenylphosphine oxide and triphenylphosphite.

Preferred ligands are selected from the group consisting of pyridinesand phosphines substituted with ionic functional groups such assulfonates, carboxylates, phosphates, ammonium or phosphonium compounds.Non-limiting examples that can be cited are:

-   1-(4-pyridyl)-2-(dicyclopentylmethylphosphonium)-ethane    tetrafluoroborate: ligand (1);-   1-(N-imidazolyl)-2-(dicyclopentylmethylphosphonium)-ethane    tetrafluoroborate: ligand (2);-   1-(diphenylphosphino)-2-(4-N-methylpyridinium)-ethane    tetrafluorophosphate: ligand (3);-   1-(dicyclopentylphosphino)-2-(3-methylimidazolium-1-yl)-ethane    hexafluorophosphate: ligand (4);-   the tetrabutyl ammonium triphenylphosphine trisulfonate ligand;-   the sodium triphenylphosphine trisulfonate ligand (or TPPTS);-   the sodium triphenylphosphine monosulfonate ligand (or TPPMS);-   (3-methylimidazolium-1-yl hexafluorophosphate)-2-pyridine: ligand    (5); and-   bis(3-methylimidazolium-1-yl hexafluorophosphate)-2,6-pyridine:    ligand (6).

The catalytic composition is obtained by mixing the ionic liquid withthe cobalt compound and the ligand, in any manner. It is also possibleto dissolve the transition metal compound and/or ligand in an organicsolvent in advance.

The complex between the cobalt precursor and the ligand can be preparedin advance of the reaction by mixing the cobalt precursor with theligand in a suitable solvent, for example an organic solvent or thenon-aqueous ionic liquid that will then be used in the catalyticreaction. The complex can also be prepared in situ by mixing the cobaltprecursor and the ligand directly in the hydroformylation reactor. It isalso possible to inject the ligand only at the depressurization stepfollowing reaction.

The concentration of the cobalt complex in the non-aqueous ionic liquidis not critical. It is advantageously in the range 0.1 mmoles per literof ionic liquid to 5 moles per liter, preferably in the range 1 mmole to1 mole per liter, and more preferably between 10 and 500 mmoles perliter. The mole ratio between the ligand and the cobalt compound is inthe range 0.1:1 to 500:1, preferably in the range 1:1 to 100:1.

Olefinically unsaturated compounds that can be hydroformylated areselected from the group consisting of mono-olefins, di-olefins, inparticular conjugated di-olefins, and olefinic compounds comprising oneor more heteroatoms, in particular from unsaturated groups such as theketone or carboxylic acid function. Non-limiting examples that can becited are the hydroformylation of pentenes to hexanal andmethylpentanal, hexenes to heptanals and isoheptanals, isooctenes toisononanals, isodecenes to iso-undecanals, and olefinic C₁₁ to C₁₆ cutsto C₁₂ to C₁₇ aldehydes. Said olefinic compounds can be used in the pureform or diluted with saturated or unsaturated hydrocarbons.

The ratio of the partial pressures of the hydrogen to carbon monoxideused in the reaction medium for hydroformylation can be 10:1 to 1:10,preferably in a ratio of 1:1, but any other ratio can be used whencarrying out the process.

The temperature at which hydroformylation is carried out is in the range30° C. to 200° C.; advantageously the temperature is below 180° C.,preferably in the range 50° C. to 150° C. The pressure can be in therange 1 MPa to 20 MPa, preferably in the range 2 MPa to 15 MPa. Examplesof particular conditions are a temperature of 95° C. and a pressure of6.5 MPa or a temperature of 140° C. and a pressure of 10 MPa.

The reaction for the catalytic hydroformylation of unsaturated compoundscan be carried out in a closed, a semi-open or a continuous system withone or more reaction stages. In a continuous implementation, theeffluent from the pressurized reactor is transferred into a vessel inwhich it is depressurized to a pressure of less than 1 MPa andpreferably to atmospheric pressure, to a temperature of at most 150° C.and preferably below 60° C. Contact between the two liquid phases can bemaintained in this step by mechanical stirring or by any other suitablemeans for example, by vigorous pumping using cocurrent or countercurrentcirculation known as “pump around” or by suction and redispersion ofdroplets by, for example, an “Ultraturax® device. The function of thestirring is to provide sufficient area for mass transfer by breaking upthe phases into droplets. Stirring during depressurization is notmandatory but is preferred. Minimum depressurization times dependsparticularly on the initial pressure, the size of the vessel, thevolatility of the products and the power of the stirring (if any duringthis step). In any case, the depressurization is conducted sufficientlyslowly and in combination with sufficient mixing of the phases, ifemployed, to transfer at least 50% (preferably at least 90%, morepreferably at least 99%) of the cobalt complex from the organic phase tothe non-aqueous ionic liquid phase. Accordingly, the contact time in thedepressurization vessel should be sufficient to ensure optimal transferof the catalyst to the non-aqueous ionic liquid phase.

At the outlet from the depressurization vessel, the organic phasecontaining the reaction products is advantageously separated simply bydecanting the non-aqueous ionic liquid phase containing almost all ofthe catalyst. At least a portion of this ionic liquid phase, whichcontains the catalyst, is returned to the reactor; the other portion canbe processed to eliminate catalyst decomposition residues.

The invention also relates to apparatus for carrying out thehydroformylation process as defined in the above description, saidapparatus comprising:

-   -   at least one reactor A1;    -   at least one depressurization vessel (“depressurizer”) B1;    -   and at least one decanter B2 to decant the polar phase        containing at least the non-aqueous ionic solvent containing at        least the catalyst which is recycled to reactor A1;        and also:    -   at least one line 1 for introducing feed to be hydroformylated        and the carbon monoxide/hydrogen mixture;    -   at least one line 2 for transferring the effluent from the        reactor to the depressurizer B1;    -   at least one line 3 for sending the mixture of the organic        effluent and the ionic solvent contained in the depressurizer B1        to the decanter B2;    -   at least one line 6 for returning the gas from the depressurizer        B1 to the reactor A1;    -   at least one line 5 for returning the polar phase containing at        least the ionic liquid and the catalyst separated in B2 to the        reactor A1;    -   at least one line 7 which can withdraw the as synthesized        reaction products from the decanter B2.

The apparatus also comprises:

-   -   in the separation section, at least one column A2 for separating        the crude reaction products from the unreacted olefinically        unsaturated compound to be hydroformylated;        and also:    -   at least one line 4 for recycling the unreacted olefinically        unsaturated compound to be hydroformylated separated in column        A2 to the reactor A1;    -   at least one line 8 which can send the products leaving from the        foot of the column A2 to the remainder of the product        fractionation train.

BRIEF DESCRIPTION OF DRAWING

The process and apparatus of the invention will be better understoodfrom the description below, made with reference to the attached drawingwhich is a schematic flowsheet.

DETAILED DESCRIPTION OF DRAWING

In the drawing, the reaction is carried out in the reactor A1 in thepresence of the feed to be hydroformylated, which can be introduced vialine 1, of a transition metal compound(s), of a Lewis base ligand (whichcan optionally be introduced as a mixture with the transition metalcompound(s)), and of a carbon monoxide and hydrogen, which can beintroduced via line 1, and in the presence of at least one non-aqueousionic liquid. The ionic liquid can be introduced into the reactor at thestart of the reaction. Optionally, fresh ionic liquid can be injectedinto the reactor A1 during the reaction and used ionic liquid can bewithdrawn from A1 (the means for injecting and withdrawing the ionicligand are not shown in the drawing).

The heat of reaction is removed by techniques that are known to theskilled person and which are not shown in the drawing.

At the outlet from the reaction section, the reactor effluent is sentvia line 2 to at least one depressurizer B1 in which the pressure isreduced. Stirring can be maintained in B1 either by mechanical means orby any other suitable means. The gas released by the depressurizationescapes via line 6 and is returned to the reactor A1 afterrecompression.

The effluent from depressurizer B1 is sent to decanter B2 via line 3. Indecanter B2, the polar phase which contains at least the ionic liquidand the catalyst is separated from the product mixture and organicsolvent is returned to the reactor A1 via line 5.

The organic phase separated out in decanter B2 is sent to a distillationcolumn A2 via a line 7. In column A2, the unreacted olefinicallyunsaturated compound to be hydroformylated is separated overhead. It isrecycled to reactor A1 via line 4. The crude reaction products collectedfrom the bottom of A2 are sent via a line 8 to a specific fractionationtrain (not shown).

The following examples illustrate the invention without limiting itsscope.

EXAMPLE 1

The hydroformylation reaction was carried out in a 300 ml stainlesssteel autoclave provided with a double jacket for regulating thetemperature by circulation of a heat transfer fluid and provided with aconventional efficient mechanical paddle—counter-paddle stirring systemgenerally operating at 250 to 2500 rpm, preferably 500 to 1000 rpm. 0.4g of dicobalt-octacarbonyl (2.3 mmole of cobalt), 1 molar equivalent ofdeaerated and distilled pyridine (Lewis base ligand), 10 ml of3-butyl-1-methylimidazolium bis(trifluoroethylsulfonyl) amide(non-aqueous ionic liquid), 30 ml of heptane and 30 ml of 1-hexene wereintroduced into the autoclave which had been purged of air and moistureand placed under 1 atmosphere of hydrogen-carbon monoxide (1:1 molar)synthesis gas. The pressure of the synthesis gas was raised to 10 MPaand the temperature was raised to 140° C. and stirring was commenced.After reacting for 3.5 hours, the synthesis gas inlet was closed and thereactor was allowed to cool to 25° C. Maintaining the stirring, thepressure was slowly released from 10 MPa to atmospheric pressure duringa period of 30 minutes. Stirring was then stopped and the reactionmixture was allowed to decant overnight. After removal from theautoclave, the upper organic phase was slightly colored.

Gas chromatographic analysis of the two phases after flashing andweighing the non flashed residues produced the material balance of thereaction. The 1-hexene conversion yield was 99.5% by weight. Theselectivity for C₇ aldehydes was 77.6% and the n/iso(n-heptanal/isoheptanals) ratio was 1.2. The organic phase contained7.3% of the totality of cobalt engaged in the reaction.

EXAMPLE 2

The hydroformylation reaction was carried out in the same apparatus andusing the same method as that described in Example 1 with the exceptionthat the autoclave was degassed without stirring. After reacting for 4hours, the autoclave was emptied. The upper organic phase was slightlycolored.

The 1-hexene conversion yield was 97.9% by weight. The selectivity forC₇ aldehydes was 85.9% and the n/iso (n-heptanal/isoheptanals) ratio was1.6. The cobalt metal content of the organic phase was 440 ppm (partsper million by weight), correspond to 12.8% of the cobalt engaged in thereaction.

EXAMPLE 3

The hydroformylation reaction was carried out in the same apparatus andusing the same method as that described in Example 1 with the exceptionthat the ligand was bis(3-methylimidazolium-1-ylhexafluorophosphate)-2,6-pyridine (1 molar equivalent with respect tocobalt) and the non-aqueous ionic liquid was 3-butyl-1-methylimidazoliumhexafluorophosphate. After reacting for 3 hours, the autoclave wasemptied. The upper organic phase was practically colorless.

The 1-hexene conversion yield was 97.7% by weight. The selectivity forC₇ aldehydes was 55.3% and the n/iso (n-heptanal/isoheptanals) ratio was0.9. The cobalt metal content of the organic phase was 15 ppm (parts permillion by weight), corresponding to 0.5% of the cobalt engaged in thereaction.

EXAMPLE 4

The hydroformylation reaction was carried out in the same apparatus andusing the same method as that described in Example 1 with the exceptionthat the ligand was sodium triphenylphosphine monosulfonate (1 molarequivalent with respect to cobalt). After reacting for 6 hours, theautoclave was emptied. The upper organic phase was slightly colored.

The 1-hexene conversion yield was 96.8% by weight. The selectivity forC₇ aldehydes was 73.7% and the n/iso (n-heptanal/isoheptanals) ratio was1.4. The cobalt metal content of the organic phase was 180 ppm (partsper million by weight), corresponding to 6% of the cobalt engaged in thereaction.

EXAMPLE 5 (COMPARATIVE)

The hydroformylation reaction was carried out in the same apparatus andusing the same method as that described in Example 1 with the exceptionthat no ligand was introduced. After reacting for 6 hours, the autoclavewas emptied. The upper organic phase was a strongly colored deep brown.

The 1-hexene conversion yield was 99.6% by weight. The selectivity forC₇ aldehydes was 18.5% and the n/iso (n-heptanal/isoheptanals) ratio was0.4. The organic phase contained 90% of the cobalt engaged in thereaction.

This comparative example shows that in the absence of a ligand,recycling the cobalt in the non-aqueous ionic liquid is compromised bythe solubility of the carbonyl complexes in the organic phase.

EXAMPLE 6 TO 10 (COMPARATIVE)

The same behavior characteristic of the absence of a ligand as shown inExample 5 was verified using a wide range of ionic liquids:

-   Example 6: 3-butyl-1-methylimidazolium tetrafluoroborate;-   Example 7: 3-butyl-1-methylimidazolium bis(trifluoromethylsulfonyl)    amide;-   Example 8: 3-butyl-2-methyl-1-methylimidazolium hexafluorophosphate;-   Example 9: 3-butyl-2-methyl-1-methylimidazolium tetrafluoroborate;    and-   Example 10: 3-butyl-2-methyl-1-methylimidazolium    bis(trifluoromethylsulfonyl) amide.

In these examples carried out without ligands, for the same conversionand the same selectivity as that obtained in Example 5, quantities ofcobalt metal in the organic phase were observed that corresponded toproportions of 70% to 100% of the cobalt engaged in the reaction.

The preceding examples can be repeated with similar success bysubstituting the generically or specifically described reactants and/oroperating conditions of this invention for those used in the precedingexamples. Also, the preceding specific embodiments are to be construedas merely illustrative, and not limitative of the remainder of thedisclosure in any way whatsoever.

The entire disclosure of all applications, patents and publicationscited above and below, and of corresponding French application-02/04563, filed Apr. 11, 2002, are hereby incorporated by reference.

From the foregoing description, one skilled in the art can easilyascertain the essential characteristics of this invention and, withoutdeparting from the spirit and scope thereof, can make various changesand modifications of the invention to adapt it to various usages andconditions.

1. An apparatus for carrying out hydroformylation of olefinicallyunsaturated compounds, said apparatus comprising: at least one reactor,Al, for reacting at least one olefinically unsaturated compound withhydrogen and carbon monoxide to form a hydroformylation effluent in thepresence of at least one non-aqueous ionic liquid, wherein said reactorincludes means for putting the reactor contents under pressure andstirring the reactor contents, and wherein the reactor contains at leastone catalyst comprising at least one complex of cobalt with at least oneligand selected from the group consisting of Lewis bases; at least onedepressurization vessel, B1, separate from the reactor Al, fordepressurizing the hydroformylation effluent sufficiently slowly totransfer at least 50% of the cobalt complex from the organic phase tothe polar phase containing the non-aqueous ionic liquid phase; and atleast one decanter, B2, for decanting the polar phase containing atleast the non-aqueous ionic solvent containing at least the catalyst forrecycling to reactor A1; the reactor, depressurization vessel anddecanter being operatively connected with one another by: at least oneline 1 for introducing said at least one olefinically unsaturatedcompound to be hydroformylated and a carbon monoxide/hydrogen mixtureinto reactor A1; at least one means for providing said at least onenon-aqueous ionic liquid in said reactor A1, at least one line 2 fortransferring the effluent from the reactor A1 to the depressurizationvessel B1; at least one line 3 for sending the mixture of the organiceffluent phase and the polar phase containing the non-aqueous ionicsolvent from the depressurization vessel B1 to the decanter B2; at leastone line 6 for returning the gas from the depressurization vessel B1 tothe reactor A1; at least one line 5 for returning the polar phasecontaining at least the ionic liquid and the catalyst separated indecanter B2 to the reactor A1; and at least one line 7 for withdrawingthe organic effluent phase containing synthesized reaction products fromthe decanter B2.
 2. An apparatus according to claim 1 furthercomprising: in communication with the at least one line 7 forwithdrawing the organic effluent phase containing synthesized reactionproducts from the decanter B2, at least one column A2 for separating thecrude reaction products from unreacted olefinically unsaturatedcompound; at least one line 4 for recycling the unreacted olefinicallyunsaturated compound separated in column A2 to the reactor A1; and atleast one line 8 for sending the products leaving from the foot of thecolumn A2 to the remainder of a product fractionation train.
 3. Theapparatus of claim 1 wherein the depressurization vessel is fordepressurizing the effluent from the hydroformylation reaction to apressure of less than 1 MPa at a temperature of at most 150° C., and thedepressurization vessel includes means for mechanical stirring toprovide contact between the two liquid phases.
 4. The apparatus of claim1, wherein the depressurization vessel is for depressurizing theeffluent from the hydroformylation reaction to atmospheric pressure. 5.The apparatus of claim 1, wherein the reactor is for carrying out thehydroformylation reaction at a temperature in the range 30° C. to 200°C., and at a pressure in the range 1 MPa to 20 MPa.
 6. The apparatus ofclaim 1, wherein the at least one depressurization vessel, B1, is fordepressurizing the hydroformylation effluent sufficiently slowly totransfer at least 90% of the cobalt complex from the organic effluentphase to the polar phase containing the non-aqueous ionic liquid.
 7. Theapparatus of claim 1, wherein the at least one depressurization vessel,B1, is for depressurizing the hydroformylation effluent sufficientlyslowly to transfer at least 99% of the cobalt complex from the organiceffluent phase to the polar phase containing the non-aqueous ionicliquid.
 8. The apparatus of claim 1, wherein the depressurization vesselincludes means for stirring the phases during depressurization.